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KIJENSKI, RADOMSKI, AND FEDORYNSKA
408
vacancies (21, 22)) play the role of acceptors for alkali- zene (Aldrich 99% , dest. bp 408–409 K and dried or o-,
metal-derived electrons (the rule of F+s centres formation). p-, m-xylenes (Aldrich, >99)) were introduced into a glass
Furthermore, reactants such as alkenes or alkylbenzenes ampoule (20 cm3) that had been evacuated and rinsed with
form with F+s centres secondary EDA complexes which are dry-deoxygenated N2. The frozen ampoule was sealed and
of high cata- lytic importance for hydrogenation (of, e.g., placed into the evacuated and pure dinitrogen-washed au-
alkenes) or dehydrogenation (of, e.g., alkylaromatic hydro- toclave. The reactor was then rinsed with ethene or propene
carbons) reactions (21, 22, 26). Finally, the above reactions and filled with a given gas to 1.01 MPa (Aldrich, 99.5+% ,
proceed through radical intermediates. The listed similari- ethene) or 0.71 MPa (Aldrich, 99.5+% , propene). The au-
ties between the catalytic systems used by Pines and solid toclave was thermostatured, the ampoule with catalyst and
superbases prompted us to investigate the catalytic activity alkylbenzene was broken, and the remaining mixture was
of superbasic catalysts in the side-chain alkylation of alkyl stirred. The reaction products were analyzed by GC using a
derivatives of benzene. This work was also intended to be a 5-m column (OV 101/Chromosorb W) and detected by MS
study of the reaction mechanism. Alkyl aromatics cumene, (HP 4890 series II).
ethylbenzene, toluene, and o-, m-, and p-xylenes were cho-
The reactions under normal pressure were carried out
sen as a model; the alkylating agents were ethene, propene, according to a similar procedure in a glass batch reactor
and trans stilbene (1,2-diphenylethene). Excellent demon- (150 cm3) under normal pressure. In this case, 1.64 mmol of
strations of effects of the appearance of the radical species corresponding alkylbenzene (0.156 g of toluene, 0.174 g of
were achieved by means of the catalyst poisoning and the ethylbenzene, 0.196 g of cumene, or 0.177 g of correspond-
ESR measurements of the adsorbed states of the reactants. ing xylene) reacted with an excess of ethene or propene
The latter is a special focus of the work of this laboratory.
over 0.05 g of superbasic catalyst (MgO–K, -Al2O3–K, or
MgO–K–polyaromatic hydrocarbon).
The reactions with ethylene oxide were carried out
in a glass batch reactor at 373 K under normal pres-
sure; 1.64 mmol of corresponding alkylbenzene (0.156 g of
toluene, 0.174gofethylbenzene, and 0.196gofcumene) was
introduced into the evacuated and then dry-deoxygenated
dinitrogen-washed reactor and filled with ethylene oxide
(Fluka, purum, >99.8% ).
EXPERIMENTAL
Catalysts
Magnesia was obtained by hydrolysis of Mg(NO3)2
6H2O with a concentrated aqueous ammonia solution.
After the solution was washed with doubly distilled water,
the Mg(OH)2 precipitate was dried at 333, 353, and 393 K
for 24 h at each temperature.
-Alumina was prepared by hydrolysis of aluminium tri-
isopropoxide (Fluka, pract. dest. 98% Al), previously pu-
rified by distillation under vacuum (bp 413 K, 1.07 kPa).
The hydrolysis procedure has been described elsewhere
(27, 28). The obtained Al(OH)3 was dried at 313, 353, and
393 K for 24 h at each temperature.
Both hydroxides were calcined before potassium evapo-
ration, first in air at 823 K for 1 h and then in a stream of
water-free and deoxygenated nitrogen at the same temper-
ature for 16 h in the case of MgO and for 5 h in the case of
-Al2O3.
Metallic potassium (Fluka, purum, 98% ) was deposited
onto magnesia and -alumina surfaces by chemical vapour
deposition evaporation under reduced pressure (1.3 Pa) at
573 K. After evaporation the catalysts were evacuated at
623 K and then cooled in a stream of water-free deoxy-
genated nitrogen.
Poisoning of Active Sites
Reactions in the presence of the free radical trap
TEMPO (2,2,6,6-tetramethylpiperydynyl-1-oksyl, Aldrich,
99% ) were performed at 373 K for 5 h in the glass batch
reactor (150 cm3) with the same amounts of reactants as
those in reactions under normal pressure described above.
Then, 0.001 g of TEMPO was introduced into the reactor
together with 0.05 g of a catalyst.
Textural Properties of Studied Catalysts
The specific surface area and pore distribution on the sur-
faces of the studied catalysts were determined by BET using
a Quantasorb IR2 apparatus (Quantachrom) (Table 1).
TABLE 1
Specific Surface Area and Predominant Pore Radius
of the Studied Carriers and Superbasic Catalysts
Reactions
SBET
Pore radius
a
The alkylation reactions under pressure were performed
in a stainless steel pressure reactor (250 cm3) according to
the following procedure: 0.25 g of catalyst and 8.2 mmol
of alkylbenzene (0.78 g for toluene (Aldrich 99% , dest.
bp 283–384 K and dried), 0.98 g for cumene (Aldrich 99% ,
dest. bp 425–427 K and dried), and 0.87 g for ethylben-
1
Catalyst
MgO
MgO–K
-Al2O3
(m2g
)
A
37
31
92
90
74
71
38
37
-Al2O3–K